Polymerization products of certain resins containing both hydroxyl and allyl radicals, and method of making same



Patented Nov. 13, 1951 POLYMERIZATION PRODUCTS OF CERTAIN RESINS CONTAINING BOTH HYDROXYL AND ALLYL RADICALS, AND METHOD OF MAKING SAME Melvin De Groote, University City, Mo., assignor to Petrolite Corporation, Ltd., Wilmington, Del. a corporation of Delaware No Drawing. Application August 8, 1950, Serial No. 177,552

1 20 Claims. The present invention is concerned with the production of certain polymerization products derived from resins containing both allyl radicals and hydroxyl radicals. Polymerization is the result of conventional polymerization reactions involving the allyl radicals. The polymerization products so obtained have peculiar properties, for example, the ability to form esters of semidrying oils or to yield surface-active derivatives by oxyalkylation. When combined with semidrying oils, products are obtained which are suitable for the manufacture of varnish and coat- 11185.

Another aspect of the invention is concerned with the method of manufacturing the herein described polymerization products. Such polymerization products can be used in other ways,

for example, by combining ethylene imine so as to yield resinous products having amine radicals, and thus, susceptible for use in ion exchange processes.

The products obtained by subjecting such polymers to oxyalkylation, and particularly oxyethylation, are described in my co-pending application Serial No. 177,553 filed August 3, 1950.

Over and above this, such oxyalkylated derivatives are suitable for breaking oil field emulsions or other emulsions of the water-in-oil type, as described in my co-pending application Serial No. 177,554, filed August 3, 1950.

The polymerized allyl radical-containing hydroxylated resins herein described are prepared especially by a five-step procedure:

(1) The preparation of phenol-aldehyde resins of the kind described in detail in U. S. Patent No. 2,499,370,'dated March '7, 1950, to De Groote and Keiser, with the following qualification:

Said aforementioned patent is limited to resins obtained from difunctionai phenols having 4 to 12 carbon atoms in the substituent hydrocarbon radical. For the present purpose the substituent may have as many as 18 carbon atoms as in the case of resins prepared from tetradecylphenol, substantially para-tetradecylphenol, as sold by the Oronite Chemical Company, San Francisco, California. Similarly; resins can be prepared from hexadecylphenol or octadecylphenol. This feature will be referred to subsequently.

(2) The second step involves treating the phenol-aldehyde resin so obtained with an alkylene oxide selected from the class of ethylene oxide, propylene oxide, butylene oxide, glycide and methylglycide in the ratio of at least one and less than two moles of allrylene oxide per phenolic hydroxyl. The preparation of such derivatives 2 is described in De Groote and Wirtel co-pending application Serial No. 99,361, filed June 15, 1949. Said co-pending application illustrates the use of resins in which the hydrocarbon substituent in the rings may have as many as 18 carbon atoms, as previously referred to.

(3) The third stepinvolves the hydrogenation of such oxyalkylated resins, i. e., the conversion of the aromatic compounds into the alicyclic analogues. The procedure employed is described in detail in co-pending application of De Groote and Keiser, Serial No. 64,443, filed December 8, 1948. In said last mentioned co-pending application the phenols employed are selected from the same class referred to in issued U. S.

Patent No. 2,499,370, but needless to say, the process is equally applicable in the class of phenols having as many as 18 carbon atoms in the substituent group, as previously described.

(4) The fourth step involves the treatment of the compounds in the presence of an alkaline catalyst with allyl glycidyl ether.

(5) The fifth and final step involves polymerization by means of a suitable reactant, such as an organic peroxide, or by oxidation of a gaseousoxygen containing medium, such as air, or a combination of such procedures, or any other conventional procedure employed for producing polymers from conventional allyl radicalcontaining materials.

Briefly stated, the present process is concerned with the process and the products obtained by the following process, to wit, the process of (a) Reacting a phenol with an aldehyde so as to yield- (b) An oxyalkylation-susceptible, fusible, organic solvent-soluble, water-insoluble phenolaldehyde resin; said resin being derived by reaction between a difunctional monohydric phenol and an aldehyde having not over 8 carbon atoms and reactive toward said phenol; said resin being formed in the substantial absence of trifunctional phenols; said phenol being of the formula:

in which R is a hydrocarbon radical having at least 4 and not more than 18 carbon atoms and substituted in the 2', 4, 6 position; subjecting said aforementioned resin to oxyalkylation with (0) An alpha-beta alkylene oxide having not swi es is more than 4 carbon atoms and selected from the class consisting of ethylene oxide, propylene oxide, butylene oxide, glycide and methylglycide; said oxyalkylated resin being characterized by the introduction into the resin molecule of a plurality of divalent radicals having the formula B10, in which. R1 is a member selected from the class consisting of ethylene radicals, propylene radicals, butylene radicals, hydroxypropylene radicals, and hydroxybutylene radicals; with the proviso that from about one-half to less than 2 moles of alkylene oxide be introduced for each phenolic nucleus;

(d) Converting said oxyalkylated resin into the corresponding alicyclic compound by hydrogenation in presence of a hydrogenating catalyst;

(e) Reacting said hydroaromatic compound with allyl glycidyl ether, with the proviso that at least 2 moles. of allyl glycidyl ether be reacted for each alicyclic molecule and not in excess of three times the number of hydroxyl radicals present in said molecule; and

(f) Polymerizing said allyl-radical-containing hydroaromatic compounds.

For purpose of convenience and also for ease of comparison with the aforementioned patent, or aforementioned co-pending applications, what is said hereinafter will be divided into five parts:

Part 1 will be concerned with the preparation of the resins;

Part 2 will be concerned with the oxyalkylation of the resins;

Part 3 will be concerned with the hydrogenation of the resins;

Part 4 will be concerned with the reaction of the alicyclic products with allyl glycidyl ether; and

Part 5 will be concerned with the polymerization of the allyl radical-containing alicyclic compounds or products described in Part 4, immediately preceding.

PART 1 Reference is made to the following U. S. patents: Nos. 2,499,365; 2,499,366; 2,499,367; 2,499,368, and 2,499,370, all dated March 7, 1950, to De Groote and Keiser. These patents describe phenolic resins of the kind herein employed as initial materials. For practical purposes, the resins having 4 to 12 carbon atoms are most satisfac tory, with the additional C14 carbon atoms also being very satisfactory, The increased cost of the C16 and C18 carbon atom phenol renders these raw materials of less importance at least, at the present time.

For specific description of such resins, referonce is made particularly to Patent 2,499,370 and to Examples 1a through 103a of that patent for specific examples of such resins.

As previo"sly noted, the hydrocarbon substituent in the phenol may have as many as 18 carbon atoms, as illustrated by tetradecylphenol, hexadecylphenol and octadecylphenol, reference in each instance being to the difunctional phenol, such as the orthoor para-substituted phenol, or a mixture of the same. Such resins are described also in issued patents, for instance, U. S. Patent No. 2,499,365, dated March 7, 1950, to De Groote and Keiser, such as Example 71a.

PART 2 As has been pointed out previously, suitable resins can be made following the procedures previously described, or, for that matter, can be purchased in the open market. The second step in the overall process involves the use of an alkyl ene oxide, such as ethylene oxide, propylene oxide and glycide. or methylglycide. The most suitable oxides from an economical standpoint are ethylene oxide or propylene oxide. Obviously, the apparatus suitable for oxyethylation is also suitable for oxypropylation and will serve, if desired, for use with glycide.

I have prepared a large number of resins of the kind described in Part 1, preceding, on a laboratory scale varying from a few hundred grams or less to somewhat larger amounts. Needless to say, they are also prepared regularly on an industrial scale. This same statement applies to the preparation of the oxyalkylated products with which this second part is concerned.

For a number of well known reasons, equipment, whether laboratory size, semi-pilot plant size, pilot plant size, or large scale size, is not, as a rule, designed for a particular alkylene oxide. Invariably and inevitably. however, and particularly in the case of laboratory equipment, the design is such as to use any of the customarily available alkylene oxides, i. e., ethylene oxide, propylene oxide, butylene oxide, glycide, epichlorohydrin, styrene oxide, etc.

Oxyethylations and oxypropylations are conducted under a wide variety of conditions, not only in regard to presence or absence of catalyst, kind of catalyst, previously decribed, but also in regard to the time of reaction, temperature of reaction. speed of reaction, pressure during reaction, etc. Oxyalkylations can be conducted at temperatures approximating the boiling point of water, or slightly above, as, for example, 115 to 120 C.

Likewise, resins can be oxyalkylated, particularly with ethylene oxide or propylene oxide, using temperatures and pressures which are comparatively high, for instance, temperatures in the neighborhood of 200 C. or in excess thereof, and pressures in the neighborhood of 200 pounds per square inch, or in excess thereof. Such oxyalkylations have been described in aforementioned U. S. Patent No. 2,499,370. Generally speaking, such procedure is employed under conditions where there are more than three points of reaction per molecule and where the amount of oxide added is comparatively high in ratio to the initial reactant. Such procedure is entirely satisfactory in the particular oxyalkylation step described in the instant part, i. e., Part 2.

However, since the amount of oxide is comparatively small, less than two moles per phenolic hydroxyl present in the resin unit, it is apparent that time is not a'factor. In other words, it is Just as satisfactory to employ a comparatively low temperature and low pressure, rather than conditions of oxyalkylation previously mentioned, which result in a rapid reaction rate. For this reason, I have employed conditions of the kind involving temperatures of about to C., and pressures of 30 to 40 pounds, or less. If an atmosphere of inert gas, such as nitrogen, is present during a reaction, needless to say, the pressures may be somewhate higher.

Such low temperature, low reaction rate oxyalkylatlons have been described very completely in U. S. Patent No. 2,448,664 to Fife et al, dated September 7, 1948.

As previously indicated, low pressure, low temperature reaction rates may require considerable time, as, for instance, in some of the subsequent examples in the neighborhood of one to two hours. Actually, at 180 to 200 C., such reaction might be conducted in ten minutes or less. In large scale, low temperature operations, the time might be somewhat longer, for instance, to 8 hours. In any event, the reaction is so comparatively short that it is of no marked significance, but it is more convenient to use these lower temperatures on a laboratory or semi-pilot plant scale.

I have used conventional equipment with two added automatic features: (a) a solenoid-controlled valve which shuts ofiE the propylene oxide in event that the temperature gets outside of a predetermined and set range, for instance, 110 to 120 C., and (b) another solenoid valve which shuts off the propylene oxide (or for that matter ethylene oxide if it is being used) if the pressure gets beyond a predetermined range, such as 25 to 35 pounds. Otherwise, the equipment is substantially the same as is commonly employed for this purpose, where the pressure of reaction is higher, speed of reaction is higher, and time ofreaction is much shorter. For reasons which are obvious in light of what has been said previously, I have not found it necessary to use such automatic controls under the conditions of oxyethylation employed in introducing such small portion of alkylene oxide. Controls could be used, if desired, and certainly would be used in high temperature oxyalkylations.

Thus, in preparing the various examples, I have found it particularly advantageous to use laboratory equipment which is designed to permit continuous oxyalkylation, whether it be oxypropylation or oxyethylation. With certain changes, as will be pointed out hereinafter, the equipment can be used also to permit oxyalkylation involving the use of glycide where no pressure is involved, except the vapor pressure of a solvent, if any, which may have been used as a diluent.

As previously pointed out, the method of using propylene oxide is the same as ethylene oxide. This point is emphasized only for the reason that the apparatus is so designed and constructed as to use either oxide.

The oxyethylation or oxypropylation procedure employed in the preparation of the oxyalkylated derivatives has been uniformly the same, particularly in light of the fact that either a continuous automatically-controlled procedure was employed, or else a short automatic method is used. Indeed, in this instance the latter is preferred. In this procedure the autoclave was a conventional autoclave made of stainless steel and having a capacity of approximately one gallon and a working pressure of 1,000 pounds gauge pressure. This pressure obviously is far beyond any requirement, as far as ethylene or propylene oxide goes, unless there is a reaction of explosive violence involved, due to accident. The autoclave was equipped with the conventional devices and openings, such as the variable-speed stirrer operating at speeds from 50 R. P. M. to 500 R. P. M.; thermometer well and thermocouple for mechanical thermometer; emptying outlet; pressure gauge; manual vent line; charge hole for initial reactants; at least one connection for introducing the alkylene oxide, such as propylene oxide or ethylene oxide, to the bottom of the autoclave; along with suitable devices for both cooling and heating the autoclave, such as a cooling jacket, and preferably, coils in addition thereto, with the jacket so arranged that it is suitable for heating with steam or cooling with water, and further equipped with electrical heating devices. Such autoclaves are, of course, in essence, smallscale replicas of the usual conventional autoclave used in oxyalkylation procedures. In some instances, a larger autoclave was used, i. e., one having a capacity ranging in the neighborhood of 1% gallons.

Continuous operation, or substantially continuous operation, was achieved by the use of a separate container to hold the alkylene oxide being employed, particularly ethylene oxide or propylene oxide. The container consists essentially of a laboratory bomb having a capacity of about onehalf gallon, or somewhat in excess thereof. In some instances, a larger bomb was used, to wit, one having a capacity of about one gallon. This bomb was equipped, also, with an inlet for charging and an eductor tube going to the bottom of the container so as to permit discharging of alkylene oxide in the liquid phase to the autoclave. Other conventional equipment consists, of course, of the rupture disc, pressure gauge, sight feed glass, thermometer connection for nitrogen for pressuring bomb, etc. The bomb was placed on a scale during use. The connections between the bomb and the autoclave were flexible stainless steel hose or tubing so that continuous weighings could be made without breaking or making any connections. This also applied to the nitrogen line which was used to pressure the bomb reservoir. To the extent that it was required, any other usual conventional procedure or addition which provided greater safety was used, of course, such as safety glass, protective screens, etc.

In using the small amounts of oxide involved in ratio to initial reactant, i. e., the phenol-aldehyde resin, one need not employ the automatic devices unless desired. Autoclaves of the kind described are equipped with automatic controls which would shut off the ethylene oxide or propylene oxide in event temperature of reaction passes out of the predetermined range, or pressure in the autoclave passes out of the predetermined range. However, in procedure of the kind herein reported, I have done nothing further than to set the inlet open so the oxide was added in approximately two hours and then proceed to let the autoclave run for a total of three hours, to insure completeness of reaction. Pressures in no instance registered more than 30 to 40 pounds and the temperatures varied from to C.

One thing must be borne in mind when operating at these comparatively low temperatures of oxyalkylation. When operating at a comparatively high temperature, for instance, between 150 to 200 C., an unreacted alkylene oxide, such as ethylene or propylene oxide, makes its presence felt in the increase in pressure or the consistency of a high pressure. However, at a low enough temperature it may happen that the oxide, such as propylene oxide, goes in as a liquid. If so, and if it remains unreacted, there is, of course, an inherent danger and appropriate steps must be taken to safeguard against this possibility; if need be, a sample must be withdrawn and examined for unreacted propylene oxide, or ethylene oxide. One obvious procedure, of course, is to oxypropylate or oxyethylate at a modestly higher temperature, for instance, to 0. Obviously, similar precautions are necessary in the case of ethylene oxide, although it is more reactive than propylene oxide.

I have found it comparatively simple to manually control the temperature of reaction by use of cooling water, steam, or electrical heat to raise or lower the temperature. It will be noted that the entire procedure herein involved is much simpler than where low pressure, low temperature, low-speed reactants are employed in an effort to bring out the introduction of a comparatively large amount of alkylene oxide. Such procedure is sometimes used, for example, in treating diols or triols with ten to twenty, or even thirty times their weight of alkylene oxide.

A word can be included in regard to the use of glycide. This is particularly pertinent, because Part 4 is concerned with a reaction involving allyl glycidyl ether, which reaction is also an oxyalkylation, broadly speaking, and involves a reactant which is comparable to glycide. This is obvious, since glycide is l-hydroxy-2,3-epoxypropane, and allyl glycidyl ether is 1-allyloxy-2,3- epoxypropane, As previously pointed out, glycide is an alkylene oxide suitable for use in reaction with phenol-aldehyde resins. If either glycide or methylglycide is employed, no appreciable pressure is involved, and no effort need be made to use equipment with automatic controls.

Indeed, in the use of a number of initial reactants with glycide, the entire equipment was used almost as if it were an ordinary piece of non-pressure laboratory equipment, since such reactions can be so conducted. Due to the high boiling point of glycide, one can readily employ a separable glass resin pot, as described in U. S. Patent No. 2,499,365, dated March 7, 1950, to De Groote et al., and ofiered for sale by numerous laboratory supply houses. Equipment of this kind has been advertised extensively in current chemical journals.

If such arrangement is used to prepare laboratory-scale duplications, then care should be taken that the heating mantle can be removed rapidly, so as to allow for cooling; or better still, through an added opening at the top of the glass resin pot or comparable vessel should be passed a stainless steel cooling coil so that the pot can be cooled more rapidly than by mere removal of mantle. If a stainless steel coil is introduced, it means that the conventional stirrer of the paddle type is changed to one of the centrifugal type, which causes the fluid or reactants to mix, due to swirling action in the center of the pot. Still better is the use of a metal laboratory autoclave of the kind previously described above, but in any event, when the initial amount of glycide is added to a resin, for example, in order to convert it into an oxyalkylated derivative, speed of reaction should be controlled by the usual factors such as (a) the addition of glycide; (b) the elimination of external heat; and (c) the use of cooling so there is no undue rise in temperature. All the foregoing is merely conventional, but is included, due to the hazard in handling glycide. As to the use of glycide as an oxyalkylating agent, see U. S. Patent No. 2,089,569, dated August 10, 1937, to Orthner et al.

The amount of catalyst used in oxyalkylation may vary from as little as A;% upto 5%. The amount may vary during the oxypropylation period, as exemplified by the addition of the catalyst at the very beginning of the reaction only and with no further addition. Needless to say, there is a comparatively high concentration of catalyst at the beginning of the reaction and a comparatively low concentration at the end; in fact, not infrequently the amount of catalyst at the end will be one-half of 1% sodium methylate, or caustic soda, or less. Catalyst can be added in termittently during the reaction period, provided suitable equipment is available. It is rather difilcult to employ such equipment on a laboratory scale, but it can be employed, of course, on a pilot plant scale or larger scale.

In the present situation, since comparatively little of the alkylene oxide was added per phenolic hydroxyl, time of reaction is not apt to be a factor. The amount of alkylene oxide may vary, for example, from one-half mole to less than two moles per phenolic hydroxyl. In other comparable oxyalkylations, as have been described in the literature, the amount of oxide added might be 50 to times this amount. Under such circumstances, it is necessary to speed up the reaction in order to finish the process within a reasonable length of time. In the present case the amount of oxide added was so small that even using a low temperature (95 to C.) and a comparatively low pressure, less than 30 or 40 pounds maximum, the reaction was complete in a very short period of time. As a convenience, I have generally added the oxide over a 3-hour period, since the apparatus was practically automatic. The amount of catalyst used was generally about 1.0% of the initial resin. Somewhat more can be used, or slightly less. If more is used, the reaction would, of course, be faster and if less is used, reaction might be a little slower. It is my preference to use a minimum amount of catalyst, rather than an excessive amount, for the reason that it is desirable to neutralize the excess alkalinity with hydrochloric acid, for example, or sulfuric acid, or phosphoric acid, and remove the inorganic salt prior to hydrogenation, as described in Part 3 succeeding.

One limitation of small-scale autoclave equipment (a gallon to a 2-gallon autoclave) is the difficulty involved in a suitable automatic device for adding a dry catalyst, such as sodium methylate, during the reaction. This presents no problem on a large scale with larger size equipment, and thus, the same operation conducted in equipment of increased capacity means that all the catalyst need not be added at once, but can be added intermittently in a predetermined amount, based on an hourly rate, or based on the addition of ethylene or propylene oxide. For instance, in a large scale operation involving equipment having about twenty-five times the capacity of the autoclave employed, arrangements were made to introduce better than a gallon of ethylene or propylene oxide (4,000 grams) per hour, along with the introduction of 20 grams of sodium methylate hourly during the operation period. The net result, as far as the final material was concerned, was the same, to wit, a residual alkaline catalyst equivalent to about /g% sodium methylate.

In the following example sodium methylate is used as a catalyst. The resin used was prepared in the manner described by reference to the a examples in Part 1. In practically every instance the resin was re-prepared in a triple amount, 1. e., using 3 moles of the phenol as a starting material. In each instance the amount of xylene employed was three times the amount used when only one mole of a phenol was employed, i. e., 300 grams. In all other respects, amount of aldehyde, etc., the procedure was the same, the weight ratios only being different. In the succeeding tables the amount of xylene resin solution is shown by weight; subtracting 300 in each instance gives the weight of the resin. For purpose of calculation the alkylene oxide added and the original phenol employed in manufac- 9 ture was used as a basis. This was more convenient than using the weight of resin obtained, because it may vary somewhat from batch to batch. The weight of the resin solution was such as to correspond with the original weight shown in Part 1. This is obvious by mere comparison. Actually, the amount was weighed on a laboratory balance which may have been inaccurate to the extent oi or /2%. This, of course, is immaterial in a procedure of the present type. Slmilarly, the ethylene oxide and propylene oxide were weighed as closely as possible, but here again the variation could have been oil. to 1%. 3-gram moles of the phenol were used to provide the resin. The amount of oxides employed are shown in the table. The amount of catalyst (sodium methylate) employed is also shown. In all instances, the temperature, as stated, was never higher than 115 C. and generally varied from 100 to 110 C. The pressure was never higher than 40 pounds per square inch, and in all instances, the reaction was complete in three hours.

Oxyethylation or oxypropylation was conducted in the usual manner, first, sweeping out the equipment with nitrogen and setting the controls as far as the addition of the oxide was concerned, but ignoring the controls as far as temperature and pressure were concerned. Any adjustment required in the matter of temperature and pressure could be made manually by examination of the gauges a few times during the entire procedure. The next step was to add the ethylene oxide or propylene oxide in such a manner that it was injected in the reaction vessel in somewhere between 2 to 2 hours, and then permitting the reaction period to extend up to 3 hours, so as to be sure all the oxide had combined. A specific example is included followed by way of illustration:

Example 1a of Patent 2,499,370, mixed with 300 grams of xylene, were used as the initial charge. To this there was added about 1% (5 grams) of sodium methylate. These ingredients were placed in the autoclave and the autoclave sealed and the automatic devices adjusted for injecting a comparatively small amount of oxide, 135 grams, in about 2% hours. The reaction was continued for a total of 3 hours, however, to be sure it was complete. This is a ratio of one mole of oxide for each initial phenolic hydroxyl involved in resin manufacture. The temperature was approximately C. and the pressure was less than 30 pounds per square inch. The final product was a viscous, semi-resinous product, being somewhat between a resin and a viscous, amber-colored fluid obtained by increased oxyethylation. In such instances where the resins employed were liquids, needless to say, further oxyalkylation .was in the direction of reduced viscosity. Some resins which were practically viscous liquids to start with, because less viscous or more towards the liquid stage. The color varied from deep red or amber, to some darker shades, and in some instances, lighter shades. The residual product was, of course, slightly alkaline.

For the purpose described in the next successive part, each particular sample was neutralized with hydrochloric acid and then the xylene eliminated by vacuum distillation. The resin or tacky, resinous liquid, or liquids, so obtained was then dissolved in ethyl alcohol and filtered to remove any inorganic salts. The xylene-free alcohol solution was used for hydrogenation, as outlined in Part 3, immediately following.

The following table illustrates a variety of suitably oxyalkylated resins. Such resins can be treated, of course, with glycide in exactly the same manner under the same conditions, with the exception that the autoclave is simply used as a reaction vessel with a condenser and without the use of pressure. However, in handling glycide I prefer to use the glass resin pot in the manner previously described. Glycide reacts very rapidly and the molecular proportions, etc., are

within the limits previously specified. The resins are identified in terms of the examples of Patent 2,499,370.

No. of Gr. Grs. oi Mols. Orig. Ratio Moi. Ex. No. Grs. Mol. Max.

Resin Phenol Oxide to Amt. of Max. Pres Time, in Xylene Repregz' Phenolic Catalyst Employed Catalyst Z f per sq. in hours 95 n Solution sented by Hydroxyl Solution 16 1a 786 3 5 1:1 Sodium methylate- 5 or 3b la 786 3 235 5% 5 9b 7a 870 3 235 5% 6 1011 8a 954 3 135 3 7 11!) 8a 954 3 200 4% 7 12b 86 954 3 235 6% 7 135 9a 846 3 135 3 6 9d 846 3 200 4% 6 9a 846 3 235 6% 6 16b 69a 1, 032 3 135 3 7 17b 69!! 1, 032 3 200 4% 7 18b 69a 1, 032 3 235 5% 7 19b 700 996 3 135 3 6 20b 700 996 3 200 4% 6 21b 700 996 3 235 5% 6 22b 70a 1, 038 3 135 3 7 23b 70a 1, 038 3 200 4% 7 24b 70a 1, 038 3 235 5% 7 25b 73a 1,122 3 135 3 8 26b 73a 1, 122 3 200 4% 8 27b 73a 1, 122 3 235 5% 8 28b 140 810 3 135 3 5 29b Me 810 3 200 4% 6 30b 14a 810 3 235 5% 5 No. of 01'. Grs. oi Mols. Orig. G M 1 Ratio Mol. Max Phenol Oxide to Amt. oi Max. Pres Time, in 1? 1 15 1 1 11 Repre- I; 5 Phenolic Catalyst Employed Catalyst T216?" per eq. in hours as S ution sented by Hydroxyl Solution l 786 3 175 3 1:1 Sodium Methylate-. V ,5, 3111's. orless it 1: 786 3 260 4% 1%:1 do 5 33b 1a 786 s 305 5% 1 411 5 Do. 34b 30 52s a 175 5 1:1 5 Do. 35!) 3a 828 3 250 4% 134:1 6 36b 35 52s a 305 5% 1%:1 a Do, 375 7a 570 a 175 a 1:1 6 D5. 380 7a 870 a 260 4% 134: 6 Do. 39b 7a 570 3 305 5% 1%:1 6 D0. 405 8a 054 a 175 a 1:1 7 Do. 410 8a 954 3 250 4% 1%:1 7 Do. 42b 85 954 3 305 5% 1%:1 7 Do. 43b 72a 7 1. 05s a 175 a 1:1 7 Do. 440 724 1,035 a 250 4% 114:1 7 Do. 45!; 72a 1,038 3 305 514 1%:1 7 D0, 460 7311 1,122 a 175 a 1:1 s 47b 730 1,122 a 250 4% 114:1 8 Do. 48b 7311 1,122 3 305 5% 1%: 1 5 Do. 495 14a 1110 a 175 3 1:1 5 D0. 50!) 145 810 a 200 4% 114:1 5 D0, 51b 1411 810 3 305 5% 1%:1 5 e no, 52b 24a 1,002 a 175 3 1:1 7 Do. 53b 24a 1,002 a 250 414 115:1 7 Do. 545 24a 1,052 a 505 514 1%:1 7 Do. 555 3411 $43 3 175 3 i=1 5 Do. 56b 34 843 a 200 4% 114:1 5 Do. 57b 34a 54a 3 305 5% 1%:1 5 Do. 580 8011 1,355 a 175 a 1:1 Do. 50b 505 1,355 3 250 4% 1%:1 10 Do. 60b 80a 1,355 3 305 514 1%:1 10 Do.

A 3 pressure in pounds per square inch and the temperature in degrees centigrade:

Example 10 Temper Temper Time Pressure ature, Time Pressure ogure, The oxyalkylated resin was the one previously 0. identified as Example 1b. This product, as prepared, contained xylene and a small amount of 3 28 1:528 {28 &3 basic catalyst. Enough concentrated hydro- 3 2% 2 1% 180 chlogctacid was addeld to tnzautrfi'iaihze the basic 5 70 ca a s. As prev ousy no e e xy ene was 50 50 110 4O removed by vacuura) dltlllgtloll at;1 temperatlunre 3%; 3 138 a? g8 not in excess of 2 uring e remova o 8: 10 12: 5 ,800 190 a 1 1 the xylene, the water 1ntroduced by the add1t1on 3.2? mg? 13 1:223 3g? of a small amount of hydrochloric acid was also 3 5g 1% eliminated together with any small excess of 3 1:760 140 11870 200 hydrochloric acid which may have been present. 3 5g 2 This residual material was then dissolved in 300 5 1:800 150 MO 11750 225 grams of ethylalcohol, i. e., an amount equal to 35%: 3 8 123 533 2% the xylene originally present. The anhydrous M 1:810 160 1:700 230 ethyl alcohol solution was allowed to stand for L 165 1.690 240 three days and then filtered so as to remove a small amount of precipitate. The amount of solution at this time was substantially the same as at the end of the previous operation, to wit, approximately 921 grams, of which 300 grams represented solvent. This was hydrogenated in two substantially equal half portions. Approximately 460 grams of the material described were placed in an autoclave along with 31 grams of Raney nickel. The amount of Raney nickel used in all instances was approximately 10%, by weight, of oxyalkylated reaction calculated on a solvent-free basis.

The apparatus employed was a stirring type super-pressure autoclave manufactured by the American Instrument 00., Silver Spring, Maryland, and described in their catalogue No. 406 as the 4% series. The instrument was, of course, equipped with all the conventional fittings. The stirring speed employed was approximately 450 R. P. M. The following table shows the time required to hydrogenate. The initial time period shows the starting period in the morning and the second and third columns show the gauge The next morning, after standing overnight, the temperature had dropped to 26 C. and the pressure to about 835 pounds. The material was then removed by draining the autoclave and then washin with approximately 400 to 500 grams of anhydrous isopropyl alcohol. The mixture of alcohols was then removed by vacuum distillation at less than C. The hydrogenated product was substantially identical in color as prior to hydrogenation, although there may have been some some bleaching effect during the hydrogenation reaction. The solubility of the material was not particularly changed in comparison to the product prior to hydrogenation. The tests for aromatic character, such as decolorization of bromine .water, indicated that the product was entirely, or nearly entirely, converted into a hydroaromatic compound.

Similar hydrogenation was conducted in which no alcohol was employed as a solvent, the resin having been added to the autoclave in a powdered form, and in such procedure the temperature of the autoclave was raised to C. before starting to introduce hydrogen. The hydrogen was introduced cautiously, being careful to see that the pressure did not go past 1900 pounds and that the temperature did not get past 235 C. The presence or absence of alcohol did not seem to matter particularly, as it was merely a choice with regard to convenience. Other alcohols can be used, such as methyl, propyl, etc. Such alcohols, of course, do cause some increase in pressure, particularly at the higher operating temperatures.

Thesame procedure was carried out in regard to all the various oxyalkylated products described in Part 2, preceding. The following table shows the example number correspondence between the oxyethylated non-hydrogenated material and the derivative obtained by hydrogenation, together with the maximum temperature, pressure, and time employed in hydrogenation. In each instance the amount of catalyst employed (Raney nickel) was approximately 10% of the solventfree powder. In some instances, low molal alcohols .were employed as solvents, and in other instances, no solvent was present. Actually, the hydrogenation procedure using Raney nickel and equipment of the kind now available is comparatively simple. In the matter of hydrogenated phenol-aldehyde resins see U. S. Patents Nos. 2,072,142 and 2,072,143, both dated March 2, 1937, and both to Ubben.

Ex. No. of Max. Pres. Time of Ex. No. of Max. 125.; cs $5.155 15531, Derivative Resm inch hours 10 1b 240 1, 870 6% 2c 2!) 250 1, 830 6 3c 30 260 1, 790 4c 40 245 1, 815 6% 56 5b 250 l, 890 6V 6c 60 260 1, 835 6 7c 70 240 1, 795 5% 8c 80 235 1, 800 5% 96 9b 230 1,730 6 4 10 10b 250 1,725 5 4 it? 313 H22 5 12 13c 13!; 240 1, 800 6 14:: 140 230 1,825 6 1:: is; a: lit 3 11 175 255 1, 790 6 1a: 1812 250 1, s 5 19c 19!) 260 1, 890 5 20 200 255 1,835 5% 21a 215 245 1,820 6% 22: 225 240 1,815 7 23c 23) 240 1, 850 7 246 246 235 1, 825 6% 256 250 236 1, 830 8 260 2st 250 1, 750 7% 27C 27!) 255 .1, 765 7% 28c 28!) 245 1, 765 65 20c 29!) 240 l, 780 5 30c 80!) 260 1, S90 6 31 315 266 1,800 6% 32 320 235 1, 805 6% 33: 330 255 1, 790 7 34 34b 255 1, 780 7% 35C 35b 240 1, 725 6% 36c 36!) 240 1, 725 6 37 37b 235 1, 830 5% 38: 381) 245 1, 820 6% 39 39b 260 1, 880 514 40c 40!? 230 l, 795 7 41 41b 250 1, 725 7% 42!! 42!) 240 1, 800 7% 43 4st 245 1, 790 5% 44c 44!: 200 1, 820 5% 45 45b 265 1, 835 6 46C 460 250 1, 850 5% 47 4711 255 1, 816 6 48C 480 240 l, 790 6' 49 49b 230 1,750 5 50 50b 260 1, 890 5 510 51b 240 1, 850 7% 52c 52!: 245 1, 730 7 53c 53!: 240 1, 865- 5% 54 540 255 1, 770 7% 55 55b 235 1, 840 5 56C 56!) 230 l, 890 5% 57c 57!: 255 1, 755 6% 58 58!) 255 1, 835 5% 590 590 240 1, 860 756 50c cob 250 1, 820 7% 61c 61!) 250 1, 850 8% 62 62!) 240 1, 795 8 As to change in physical appearance as a result oi hydrogenation, attention is directed to what has been said preceding. Hydrogenation in numerous cases does show some-bleaching eifect.

The hydrogenated product freed from solvent which would be susceptible to reaction with glycidyl allyl ether, was admixed with approximately 300 grams of xylene and approximately 1% of sodium methylate. Needless to say, the alcohol employed as a solvent, and for that matter, the xylene employed in Part 1 as a solvent, could be replaced by a solvent which would not be objectionable either from a standpoint of hydrogenation or oxyalkylation', as, for example, decalin. Again, as has been pointed out, all the reactions involved can be conducted in absence of any solvent. This is purely a matter of convenience.

In noting the size of the batch subjected to reaction with allyl glycidyl ether, no account is taken for increase in weight, due to hydrogenation, for the reason that this is a comparatively small factor and there have been some losses in filtering, and otherwise. Therefore, the figures that appear in the next part, i. e., Part 4, correspond. in essence, to the figures appearing in Table II, which show the grams of xylene solution; plus the oxide added. Actually, the treatment with allyl glycidyl ether, as previously noted, is an oxyalkylation process, and the reaction is conducted in the same manner as previously mentioned, and is substantially the same as one would conventionally employ in the use of glycide.

PART 4 r As previously indicated, the present part is concerned with the reaction between allyl glycidyl ether and the alicyclic compounds obtained in the manner described in Part 3, immediately preceding. Such alicyclic compounds are polyhydroxylated, having at least three or more hydroxyl radicals per molecule. Generally speaking, the number of hydroxyl radicals, if obtained by the reaction of ethylene oxide or propylene oxide, for example, would run from 3 to 7 or 8, unless the resin, prior to hydrogenation, had been treated in such a manner as to have present a greater number of phenolic hydroxyls, such as a condensation reaction to increase the resin molecule size. Obviously, if glycide or methyl glycide were used, the number of hydroxyl radicals would be substantially larger, for instance, 10, 15, 20 or even more. In any event, the amount of allyl glycidyl ether employed is suflicient to convert at least a plurality'of hydroxyl radicals per molecule into the corresponding allyl compound and may be enough to convert all hydroxyls present, or two or three times this molal amount. More allyl glycidyl ether can be employed than corresponds to the molal proportion based on hydroxyl radicals present, for the simple reason that at each stage of reaction a hydroxyl is obtained, which, in turn, is susceptible to further oxyalkylation with any alkylene oxide, and, of course, with allyl glycidyl ether.

The use of allyl glycidyl ether, as previously noted, involves substantially the same procedure and equipment as glycide. The glass equipment previously described could be used, although I have found it more convenient to employ the larger laboratory autoclave previously described. The use will be illustrated by the following examples.

As to further information in re ard to allyl w 15 glycidyl ether, see Information Sheet DS-48-22 1 Shell Development Co., Emeryville, California.

Example 1d The same piece of equipment was employed as previously described in Part 2, i. e., an autoclave, although in the instant procedure'involving the use of allyl glycidyl ether, there was no pressure involved and certain changes were made, as noted subsequently. The autoclave was equipped with a water-cooled condenser, which was shut oil when used as an autoclave. It was equipped also with a separatory funnel and an equalizing pres sure tube so the liquid, such as allyl glycidyl ether, could be fed continuously at a drop-wise or faster rate into the vessel, and the rate was controlled by visual examination. For convenience, this piece of equipment is referred to as an autoclave, because it is essentially designed for such use, but it is to be noted that it is not so used when allyl glycidyl ether, or for that matter, glycidol, was employed as described in Part 2, preceding.

There were charged into the autoclave 921 grams of a xylene solution (containing 300 grams of xylene) identified as Example 10, preceding. Such amount of sodium methylate equivalent to about 1% of the hydroxylated reactant, was added as a catalyst, which, in this instance, was 6.5 grams. The autoclave was sealed, swept with nitrogen gas and stirring started and heat applied immediately. The temperature was allowed to rise to 123 C. The allyl glycidyl ether employed was the technically pure product supplied by the Shell Development Co., Emeryville, California.

The hydroxylated reactant present in the autoclave represented approximately 3 moles of phenol when calculated back to the initial reactants described in Part 1. The amount of allyl glycidyl ether added was approximately 3 moles or 350 grams. This was added over a 3 /2 hour period. This was charged into the upper reservoir vessel, which had been flushed out previously with nitrogen and was, in essence, the equivalent of a separatory funnel. The oxide was started slowly into the reaction mass at a drop-wise rate. The reaction started immediately and the temperature rose approximately 13 to 19. Cooling water was run through the coils so the temperature for the addition of the oxide was controlled within the range oi to C. The reaction took place at atmospheric pressure, with simply a small stream of nitrogen passing into the autoclave at the very top, and passing out of the open condenser so as to avoid any possible entrance of air. Under such operation there was, of course, some loss of xylene, but examination revealed no loss or the oxide.

The product, so obtained, was fluid, lighter in color than the initial example, and on'examination. was found to be comparatively free from unreacted oxide. Likewise, examination by determination of the hydroxyl number showed substantial completeness of reaction. Needless to say, such procedure also increased the water solubility of the product.

What is said in this instance in regard to physical properties applies, for all practical purposes, to all examples obtained. Obviously, where increased amounts of the ether were employed, the final product tended to show more and more the characteristics of a viscous liquid comparable to castoroil or slightly blown castor oil. The color also decreased as more oxide was added.

Example 2d The same procedure was employed as in Example 1d, preceding, using the same operating procedure and substantially the same temperature range, with this difference: The product subjected to treatment with allyl glycidyl ether was the hydroxylated compound identified as Example 2c, preceding. The amount employed in this instance was 986 grams, including 300 grams of solvent. The amount of sodium methylate used as a catalyst was 7 grams. In all other respects, the operating procedure was identical with the two preceding examples.

Operating data in regard to similar examples are givenin the tables immediately following.

Incidentally, it is to be noted that one need not use sodium methylate as a catalyst, but can use any one of a number of other suitable catalysts, such as caustic soda or caustic potash. Stannic chloride or boron fluoride ether complex are also satisfactory.

E N f gl nt. f lvlollaaiigtio x. o. o icyc lo 0 to Ex. Alicyclic Compound Solvent Amt, Cam] st Amt each Mole ag- 5 Time of No. Compound Used (Solgrs. y grs. Phenol R Reaction Used vent-tree Originally we basis), grs. present 14 1c 621 300 Sodium Methylate 6:5 360 1:1 Not over 138. 3 211 2c 686 300 .do 7% 360 1:1 do 2' 3d 30 721 300 7% 350 1:1 2% 4d 10c 789 300 8 350 1:1 4 5d no 854 300 9 350 1:1 3% 6d 120 889 300 9 350 1:1 3% 7d 867 300 9 350 1:1 3 8d 932 300 10 350 1:1 2% 9d 19:: 967 300 10 360 1:1 4 10d 250 957 300 10 350 1:1 4 1111 260 1,022 300 10 350 1:1 4' 12d 270 1, 057 300 11 350 1:1 3% 13d lo 621 300 7 260 3:4 2 14d 20 686 300 7 260 3:4 2 15d 36 721 300 7 260 3:4 2 16d 100 789 300 8% 260 3:4 3 17d llc 854 300 9 260 3:4 3% 18d 120 889 300 10 260 3:4 4% 19d 17:: 867 300 9 260 3:4 4 2011 180 932 300 9% 260 3:4 4% 21d 967 300 10 260 3:4 3% 22d 25!: 957 300 10 260 3:4 4 23d 26c l, 022 300 10 260 3:4 4% 24d 270 1, 057 300 11 260 3:4 3% 2511 37c 745 300 8 350 1:1 3% 26d 380 830 300 9% 350 1:1 4 27d 390 875 300 9 350 1:1 3% 28d 49:: 685 300 7 350 1:1 3 29d 500 770 300 8% 850 1:1 3 30d 51c 815 300 8% 350 1:1 2

17 Attention is again directed to the fact that other suitable solvents other than xylene may be used, such as decalin, cymene, etc. Other suitable catalysts can be employed. It is also pointed out that the amount of allyl glycidyl ether employed need be only enough to introduce a plurality of allyl radicals per resin molecule, or may be enough to introduce a number of allyl radicals equal to the original phenolic hydroxyls, or twice as many, or three times as many. My preferred ratio is to use 3 moles of allyl glycidyl ether for each 4 moles of phenol originally used, or to use an equal number of moles, 4 for 4, or else 5 moles of allyl glycidyl ether for each 4 moles of phenol originally used.

PART 5 The allyl radical-containing products are polymerized in much the same way as comparable products, for instance, castor oil, dehydrated castor oil, allyl sucrose, or the like, are polymerized or thickened or bodied. Such polymerization is due essentially to the allyl groups undergoing allyl or vinyl condensation, or polymerization. Such vinyl polymerization is usually induced by use of a peroxide catalyst, such as benzoyl peroxide or blowing with a gaseous oxygen-containing medium, or by using a combination of the two procedures.

In any event, the usual steps are taken to free the compound from any solvent, such as xylene, which may be present and also to render it as nearly neutral as possible and to remove any inorganic salts which would tend to separate out. A slight basicity, due to the presence of a basic tertiary amine, is desirable in connection with the use of a peroxide. This applies whether the peroxide is used for partial polymerization, followed by blowing with air, for example, or is responsible totally for the polymerization. This practice, i. e., the use of a tertiary amine to act as an activator in peroxide, for instance, benzoyl peroxide, to induce polymerization is well known. Tin chloride seems to have similar properties, but is not as satisfactory. For a number of reasons, oxidation by means of air alone seems to be the simplest and the most satisfactory procedure.

Briefly stated, then, the various products identified as Examples id through 30d in Part 4, preceding, are neutralized with sufiicient concentrated hydrochloric acid to make them neutral. Any sodium chloride formed is removed by filtering. The product is then subjected to vacuum distillation which removes the xylene used as a solvent and also any water formed during the neutralization step. The final product varies from a semi-viscous liquid to a viscous or tacky liquid, or a product which exhibits almost a solid state at ordinary temperature. In all instances, these products are fluid at the temperature employed for polymerization, for instance, 110 to 150 0. Previous reference has been made to the fact that polymerization with air is comparable to the procedure that is used in obtaining an oxidized oil or blown oil, or a polymerized castor oil from castor oil or similar materials, as, for example, allyl sucrose. Such products are produced by the common practice of blowing or oxidizing the polymerizable material by means of a gaseous medium, such as air, oxygen, ozone, or ozonized air. The gaseous medium, such as air, may be moist or dry and the oxidation, or better still, polymerization. may take place in presence or absence of a catalyst. The catalyst may be of a metallic type, such as lead ricinoleate, cobalt ricinoleate, manganese ricinoleate, etc., or it may be of an organic type which produces a peroxide, such as alphapinene, linseed oil, etc. Similarly, as previously noted, peroxides themselves, such as benzoyl peroxide, or similar peroxides, may be employed as catalysts or to inhibit the incipient stage of polymerization. Such peroxide catalyst may be used in presence of a basic tertiary amine, as previously noted. The amount of catalyst may vary from as little as one-tenth of 1%, to 1%, or somewhat less. The amount of tertiary amine employed in connection with the peroxide, is usually in approximately the same order of magnitude, i. e., one-tenth of 1% up to 1%. Examples of such tertiary amines include tributylamine, triamylamine, tricyclohexylamine, etc.

Polymerization can be induced by oxidation at atmospheric pressures or super-atmospheric pressures, i. e., pressures up to or including 200 pounds gauge pressure, and at temperatures from slightly above the boiling point of water, up to any temperature that does not produce undue decomposition by pyrolytic reaction.

The time of polymerization, as induced by blowing or oxidation, may be fairly brief, for example, less than 25 hours, particularly if such oxidation takes place in conjunction with the use of a peroxide, such as acetyl peroxide or benzoyl peroxide. On the other hand, in some instances, using a temperature of approximately C., it is sometimes necessary to blow the mixture for as long as 125 to hours.

Not infrequently there is a change in the index of refraction of products during the polymerization stage. In other words, as the allyl radicals disappear, due to polymerization, there is an increase in the index of refraction. Under any particular set of conditions a study of such index of refraction may be helpful in controlling the polymerization, although as a rule, viscosity is equally satisfactory insofar that no efiort is made to reach an exact quantitative point in the polymerization range. Generally speaking, I have attempted to prepare compounds having at least three different degrees of polymerization. One stage is where there has been a noticeable increase in viscosity and the difference is substantially comparable to the difference between heavily blown castor oil and ordinary castor oil; the second stage is the point where the product begins to show incipient stringiness. This is probably where incipient gelation or cross-linking starts to take place. The third stage is where stringiness is not only obvious, but a solution of the polymerized solution in xylene, for instance. a 50% solution, still shows stringiness, but is still soluble. It is to be noted that the ultimate product, whether below the stringy stage, or in the incipient stringy stage, or at the stage where even a 50% solution in xylene is stringy, must be soluble in an organic solvent, such as xylene, low molal alcohols, decalin, diethylether of ethylene glycol, cyclohexanal, or the like. If the product is not soluble in any one of the common hydrocarbon or oxygenated solvents, it is not satisfactory for the herein described processes.

Polymerization is illustrated by the following examples:

Example 16 A product of the kind identified as Example 1d in Part 4, preceding, was freed from inorganic solvents and salts. The product was substantially neutral. 1500 grams of the product were placed in an ordinary 3-liter flask. The air terminal inlet was provided with a device which gave a multiplicity of small, fine bubbles. This was accomplished by means of a porous ceramic tube fitted to glass and available from various laboratory supply houses. The input of air was such that there was a continuous stream of air passing through the reaction mass sufllcient to provide at least moderate agitation. The temperature was raised to 138 C., and then air was passed through for 117 hours. During approximately the first third of the period, i. e., for the first 40 hours, there did not seem to be any particular change.

During the second 40 hours the material began to darken and was almost blackish-red at the end of 80 hours. By this time there was a modest but appreciable change in viscosity, even though not so marked as at the end of the final reaction period. Viscosity, of course, could not be Judged satisfactorily when the material was hot, but when the reaction mass was allowed to cool and the viscosity compared with that of the initial reaction mass at the same temperature, for instance, room temperature, it was obvious that a thickening somewhat suggestive of the change that takes place when castor oil is converted into a light blown castor oil, had taken place.

At the end of the final period the viscosity of the product had greatly increased and was suggestive of that of heavily blown castor oil. The initial product showed a viscosity more comparable to ordinary castor oil. This product was considered a characteristic as being the result of mild blowing or mild polymerization. Note what is said in regard to such characterization in subsequent Example 7e.

Example 2c The same procedure was followed in every way as in Example 1e, except that the initial charge was 1500 grams of a product identified a Example 2d in Part 4, preceding. The temperature of polymerization, the time period, the change in the product, change in color, final viscosity. etc., were substantially comparable to Example 1e, preceding.

Example 3e The same procedure was followed in every way as in Example le, except that the initial charge was 1500 grams of a product identified as Example 3d in Part 4, preceding. The temperature of polymerization, the time period, the change in the product, change in color, final viscosity, etc., were substantially comparable to Example 1e, preceding.

Example 4e The same procedure was followed in every way as in Example 1e, except that the initial charge was 1500 grams of a product identified-as Example 28d in Part 4, preceding. The temperature of polymerization, the time period. the change in the product. change in color, final viscosity, etc., were substantially comparable to Example le', Preceding. I

Example 5e The same procedure was followed in every way as in Example le, except that the initial charge was 1500 grams of a product identified as Example 2941, in Part 4, preceding. The temperature of polymerization, the time period, the change in the product, change in color. final viscoeity, etc., were substantially comparable to Example 1e. preceding.

Example 6e The same procedure was followed in every way as in Example 1e, except that the initial charge 5 was 1500 grams of a product identified as Example 30d, in Part 4, preceding. The temperature of polymerization, the time period, the change in the product, change in color, final viscosity, etc., were substantially comparable to Example 1e, preceding.

Example 7e The same procedure was employed as in Examples 1e through 6e, preceding, except that a stirring device was included in the reaction flask along with the distributing unit. In this case the temperature was held at slightly less than in the previous six examples, 1. e., at about 136 C. The stirring device apparently gave better oxidation, which, in turn, resulted in more eifective polymerization. At the end of the hours the product was not only stringy, but when mixed with an equal weight of xylene, the 50% xylene solution, so obtained, showed stringiness. In fact, the product, prior to dilution in xylene, was

-' even more than stringyit was somewhat rubbery. I have characterized the product which is blown .just short of the rubbery or stringy stage, as exemplified by Examples 1e to 6e, preceding, as being mildly oxidized, or mildly blown, or mildly polymerized.

I have used the expression "drastically oxidized to indicate a product which is not only stringy or rubbery as such, but also is highly viscous and shows stringiness or rubberiness in the 50% xylene solution. Such stage is typified by the present example, i. e., Example 7e.

Examples 8e to 12s The same procedure, 1. e., the production of a drastically-polymerized product, was applied to Examples 2d, 3d, 28d, 29d, and 30d, in the same manner as described in Examples 2e through 66, inclusive, except that the stirring device was used in each instance and in no case was a temperature higher than 140 C. employed. In each instance the final products were dark, stringy, or almost rubbery and showed stringiness or rubberiness in a 50% solution of xylene.

Example 13c The same procedure was employed in every respect as in Examples 1e, through 7e, preceding, and the particular procedure employed was the use of the stirring device, as described in Example 7e. The initial charge as before was 1500 grams of the product identified as Example 1d. The temperature of polymerization was again within the range of to C.

In this example, and in the subsequent five examples, the time period was less than in Examples 7e to 12e, inclusive. In the instant example it was 82 hours. This product, at the end of this period, showed a definite tendency to string or rubberize, but this property practically disappeared when a 50% solution in xylene was prepared. I have referred to this particular stage as being semi-drastically-oxidized to indicate a product which shows incipient stringiness, as such, but where such stringiness disappears on dilution, as previously noted.

Examples 13s to 18s, inclusive The same procedure was followed as in Example l3e, preceding, 1. e., a procedure employed so as to produce a semi-drastically-polymerized product and the products subjected to polymerization where thus identified as Examples 2d, 3d, 28d, 29d, and 30d, in Part 4, preceding.

Actually blowing or polymerizing can be conducted with ozone or ozonized air, as well as air which may or may not have its moisture content eliminated. In this particular type of reaction I have found no advantage in going to any added cost in regard to the oxygenating procedure which initiates polymerization.

The same is true of a catalyst, such as lead, manganese or cobalt naphthenate or the like, as has been described in theliterature previously mentioned. Such catalyst, in comparatively small amounts, one-tenth percent or.preferably less, will speed up the polymerization, but here again I have not found this particularly desirable. Since it is usually intended to stop the polymerization at some particular point by the use of a mild blowing or a semi-drastic blowing, or i a drastic blowing, it is of greater convenience to approach the end point slowly, rather than rapidly, and also to have polymerization cease when the air stream stops.

As I have pointed out previously, the period of oxidation can be controlled in various ways; for instance, a higher temperature can be used, or more air will be forced through the mass; more violent agitation can be employed; and most important of all, if desired, one can shorten the socalled incubation period by use of a peroxide alone, or a peroxide in combination with a tertiary amine. My experience indicates that in many instances there are present materials which appear to inhibit the polymerization step, possibly a trace of phenolic compounds. Oxidation appears to counteract or destroy these products slowly and then an incubation period seems to develop where peroxide, or the like, is built up. After this stage, polymerization takes place comparatively rapidly. This conforms to the pattern of other ,comparable polymerizations involving allyl compounds. I have been able to cut down the time required in preparation of products characterized by Examples 1e through 18c, preceding, by doing nothing more than adding about one-fourth of a benzoyl peroxide and blowing until incipient viscosity change takes place. If this did not appear in the first ten hours, I then added a second equal portion of benzoyl peroxide and repeated. Usually, the first addition of henzoyl peroxide, or a slightly larger amount, was sufficient. In some instances, I have made an addition of a third portion of benzoyl peroxide, but it has been exceptional that this has been required. Actually, all the various stages of polymerization can be obtained by the use of a peroxide-induced polymerization, in a fourth or a third or in one-half the time required by air alone.

The final products obtained by these procedures varied from heavily viscous liquids to semi-rubbery, or almost rubbery, or, in fact, rubbery solids, or semi-solids, which in each and every instance, were soluble in an organic solvent, as previously described. Needless to say, oxidation can be conducted in any convenient size reaction vessel; in fact, in a flask smaller than a 3-liter flask. This size is used simply as a matter of convenience.

I have previously pointed out that the products so obtained have utility for processes other than being subjected to oxyalkylation.

Having thus described my invention, what I claim as new and desire to secure by Letters Patent is;

1. The process of (a) subjecting an oxyalkylation-susceptible, fusible, organic solvent-soluble, water-insoluble phenol-aldehyde resin; said resin being derived by reaction between a difunctional monohydric phenol and an aldehyde having not over 8 carbon .atoms and having one functional group reactive towards said phenol; said resin being formed in the substantial absence of phenols of functionality greater than two; said phenol being of the formula:

in which R is a hydrocarbon radical having at least 4 and not more than 18 carbon atoms and substituted one of the positions ortho and para to oxyalkylation with (a) an alpha-beta alkylene oxide having not more than 4 carbon atoms and selected from the class consisting of ethylene oxide, propylene oxide, butylene oxide, glycide and methylglycide; said oxyalkylated resin being characterized by the introduction into the resin molecule at the phenolic hydroxyls of a plurality of divalent radicals having the formula R10, in

which R1 is a member selected from the class consisting of ethylene radicals, propylene radicals. butylene radicals, hydroxypropylene radicals, and hydroxybutylene radicals; with the proviso that from about one-half to less than two moles of alkylene oxide be introduced for each phenolic nucleus; (b) converting said oxyalkylated resin into the corresponding alicyclic compound by hydrogenation in presence of a hydrogenating catalyst; (c) reacting said hydroaromatic compound with allyl glycidyl ether, with the proviso that at least 2 moles of allyl glycidyl ether be reacted for each alicyclic molecule and not in excess of three times the number of hydroxyl radicals present in said molecule; and (d) polymerizing said allyl radicalcontaining derivative to yield an organic solvent-soluble product.

2. The process of claim 1, wherein the aldehyde is formaldehyde.

3. The process of claim 1, wherein the aldehyde is formaldehyde and. the alkylene oxide is ethylene oxide.

4. The process of claim 1, wherein the aldehyde is formaldehyde and the alkylene oxide is ethylene oxide, with the proviso that the molal ratio of ethylene oxide to initial phenolic hydroxyl be approximately 1 to 1.

5. The process of claim 1, wherein the aldehyde is formaldehyde and the alkylene oxide is ethylene oxide, with the proviso that the molal ratio of ethylene oxide to initial phenolic hydroxyl be approximately 1 to 1, and with the further proviso that the molal ratio of allyl glycidyl ether to the corresponding alicyclic hydroxyl be approximate- 13 1 to l.

6. The process of claim 1, wherein the aldehyde is formaldehyde and the alkylene oxide is ethylene oxide, with the proviso that the molal ratio of ethylene oxide to initial phenolic hydroxyl be approximately 1 to l, and with the further proviso that the molal ratio of allyl glycidyl ether to the corresponding alicyclic hydroxyl be approximately 1 to 1; and with the final proviso that the radical R is a butyl radical.

7. The process of claim 1, wherein the aldehyde is formaldehyde and the alkylene oxide is ethylene oxide, with the proviso that the molal ratio of ethylene oxide to initial phenolic hydroxyl be approximately 1 to 1, and with the further proviso that the molal ratio of allyl glycidyl ether to the corresponding alicyclic hydroxyl be approximatel 1 to 1; and with the final proviso that the radical R is an amyl radical.

8. The process of claim 1, wherein the aldehyde is formaldehyde and the alkylene oxide is ethylene oxide, with the proviso that the molal ratio of ethylene oxide to initial phenolic hydroxyl be approximately 1 to 1, and with the further proviso that the molal ratio of allyl glycidyl ether to the corresponding alcyclic hydroxyl be approximately 1 to 1; and with the final proviso that the radical R is an octyl radical.

9. The process of claim 1, wherein the aldehyde is formaldehyde and the alkylene oxide is ethylene oxide, with the proviso that the molal ratio of ethylene oxide to initial phenolic hydroxyl be approximately 1 to 1, and with the further proviso that the molal ratio of allyl glycidyl ether to the corresponding alicyclic hydroxyl be approximately 1 to 1; and with the final proviso that the radical R is a nonyl radical.

10. The process of claim 1, wherein the aldehyde is formaldehyde and the alkylene oxide is ethylene oxide, with the proviso that the molal ratio of ethylene oxide to initial phenolic hydroxyl be approximately 1 to 1, and with the further proviso that the molal ratio of allyl glycidyl ether to the corresponding alicyclic hydroxyl be approximately 1 to 1; and with the final proviso that the radical R is a tetradecyl radical.

11. The product obtained by the process defined inclaim 1.

12. The product obtained bythe process defined in claim 2.

13. The product obtained by the process defined in claim 3.

14. The product obtained by the process defined in claim 4.

15. The product obtained by the process defined in claim 5.

16. The product obtained by the process defined in claim 6.

17. The product obtained by the process defined in claim '7.

18. The product obtained by the process defined in claim 8.

19. The product obtained by the process defined in claim 9.

20. The product obtained by the process defined in claim 10.

MELVIN DE GROOTE.

REFERENCES CITED UNITED STATES PATENTS Name Date Wiles Nov. 7, 1950 Number 

1. THE PROCESS OF (A) SUBJECTING AN OXYALKYLATION-SUSCEPTIBLE, FUSIBLE, ORGANIC SOLVENT-SOLUBLE, WATER-INSOLUBLE PHENOL-ALDEHYDE RESIN; SAID RESIN BEING DERIVED BY REACTION BETWEEN A DIFUNCTIONAL MONOHYDRIC PHENOL AND AN ALDEHYDE HAVING NOT OVER 8 CARBON ATOMS AND HAVING ONE FUNCTIONAL GROUP REACTIVE TOWARDS SAID PHENOL; SAID RESIN BEING FORMED IN THE SUBSTANTIAL ABSENCE OF PHENOLS OF FUNCTIONALITY GREATER THAN TWO; SAID PHENOL BEING OF THE FORMULA: 